System and method for obtaining hydrocarbons from organic and inorganic solid waste

ABSTRACT

This invention relates to a system for obtaining hydrocarbons from organic or inorganic solid waste, wherein said system comprises: an inlet chamber, within which is a mixer assembly which mixes and conveys the waste through said chamber, which is also at ambient temperature, thus avoiding any thermal shock to the solid waste for processing; a dehydration chamber with a mixing assembly therein, and the upper part of this chamber contains an expansion chamber for promoting more efficient molecular breakdown; the thermal breakdown is carried out in two reactors which are operated at different temperatures, the first thermal disassociation reactor which has inside a mixer unit, and which in its upper part houses an expansion chamber, the second thermal breakdown reactor, therein has a mixer unit, and in the upper portion thereof houses an expansion chamber and at the top end thereof a vertical expansion tower; wherein the thermolytic steam is homogenized, a separator of heavy hydrocarbons, which does not require an additional cooling system, a multiple valve determines the temperature and oxygen content of the vapors and conveys them to the expansion tower in order to optimize the production of hydrocarbons, and to obtain a liquid hydrocarbon with high heating value.

APPLICATION CROSS-REFERENCES

This application claims priority from International Application NumberPCT/MX2006/000153 filed on Dec. 20, 2006 and published in Spanish.

FIELD OF THE INVENTION

The present invention is in the petrochemical, environmental,mechanical, and electrical field because it provides an apparatus andmethod to obtain hydrocarbons from solid recycling waste or residues,organic or inorganic, to obtain liquid, solid, and gaseous hydrocarbons.

BACKGROUND

Various devices, apparatuses and methods for obtaining hydrocarbons fromsolid waste by pyrolysis or thermolysis are known, in which a reactionchamber is used where the solid waste is placed, and inside of whichthere is an endless screw to convey the waste through the reactionchamber; this endless screw having the limitation that it cannot conveymetallic waste, glass, rocks, and so forth, since in addition to notbeing susceptible to the thermolysis or pyrolysis, these damage theendless screw, causing blocks, this event thereby affecting thesetechnologies' process to obtain hydrocarbons. Patent applicationWO2005044952 refers to an apparatus to process waste that has acylindrical vacuum reactor that, when heated from 250 to 410° C.,subjects the matter to be processed to a thermal shock, producingdioxins and other contaminant compounds inside the reactor, thus thisapplication differs because there is not a thermal shock of the matterfor processing since the organic and inorganic solid waste inletcylinder is not pre-heated, they remain at ambient temperature, thuspreventing the thermal shock which would produce these harmfulsubstances. It also expresses that it comprises an endless screw toremove the mixture within the reactor, this endless screw turning inonly one direction accumulates waste at one point and is jammed, whichprevents the thermal dissociation of the waste.

U.S. Pat. No. 5,720,232 relates to a method and apparatus to processwaste tires that are placed in a chamber where vacuum is brought aboutto induce pyrolysis from 176.6 to 343.3° C., the chamber includes avapor collector, the mixture of gas and liquid extracted is separated ina liquid condenser and the tire bits are removed by an endless screw.The apparatus also includes three filling chambers, a transformationreactor and carbon extraction. That apparatus only processes waste tireswhile our system processes any waste material organic or inorganic.

DESCRIPTION OF THE INVENTION

The present invention relates to a system and semi continuous processfor obtaining solid, liquid, and gaseous hydrocarbons from the thermaldissociation of solid organic and inorganic waste, the characteristicdetails of which are clearly shown in the following description andaccompanying figures, and an illustration of it and following the samereference numbers to indicate the parts and figures shown.

BRIEF DESCRIPTION OF THE FIGURES

FIG. 1 illustrates a schematic view of the machine to obtainhydrocarbons from solid waste, organic and inorganic of the presentinvention.

FIG. 2 is a perspective view of the mixing assembly.

FIG. 3 is a schematic section of the interior of the cylinder, which isthe base for the chambers and reactors.

FIG. 4 is perspective view of the intake chamber of the organic andinorganic solid waste of the referenced machine for obtaininghydrocarbons.

FIG. 5 is a perspective view of the dehydration reactor of the machineof the present application.

FIG. 6 is a perspective view of the first thermal dissociation reactorof said machine herein referenced.

FIG. 7 is a perspective view of the second thermal dissociation reactorof said machine.

FIG. 8 is a perspective view of the extractor cylinder of the solidportion of the thermal dissociation of the machine.

FIG. 9 is a perspective view of the cooling and extraction cylinder ofthe solid fraction of the thermal dissociation of the machine.

FIG. 10 is a perspective view of the heat exchangers and the separatorof heavy hydrocarbons of the processing machine of this application.

FIG. 11 is a perspective view of the separators of light hydrocarbon ofthe machine.

FIG. 12 is a perspective view of a multiple valve of the referencedmachine.

FIG. 13 is a detailed perspective view of the vacuum pumps of thereferenced machine.

FIG. 14 is a perspective view of a gas-purifying receptacle.

FIG. 15 is a perspective view of the heat exchanger and water separatorand vacuum pump of the machine.

FIG. 16 is a perspective view of a gas-purifying container, a gasfilter, and gas storing reservoir of the machine.

With reference to said figures the system to obtain hydrocarbons fromorganic and inorganic solid waste of the present invention is basicallycomprised of: a hopper 15, a solid, organic and inorganic waste intakechamber 11, a dehydration reactor 2, two thermal dissociation reactors 3and 4 respectively, a solid fraction extraction of the thermaldissociation chamber 6, a chamber 7 for cooling of the solid fraction ofthe thermal dissociation, a cylinder for the separation of heavyhydrocarbons 110, two thermolytic vapor heat exchangers 95 and 96, twocylinders to separate light hydrocarbons 116, and 117, a cylinder toseparate the liquids 139, a third heat exchanger for water vapor 138,two synthetic gas purifying reservoir 129, 141, a gas filter 145, asynthetic gas accumulating reservoir 146, three vacuum pumps 127, 128,and 140, a multiple valve 55;

The hopper 15 enables the intake of the organic and inorganic solidwaste formed by a funnel-shaped inverted cylinder, which in its upperopening 16, a ring 19 is affixed on the top rim of said hopper which, inits interior edge with a 10° perimetral cut-in resembling a conicalring, which allows the lid 20 to sit, said solid cylindrical lid 20located above this ring 19, which at the same time has a 10° cut-in onits inferior end so that when it couples with the ring 19 there is aperfectly hermetic seal, this lid at the same time has a hermetic sealand sliding mechanism 74, that allows the intake of waste into thehopper 15; wherein said mechanism comprises a handle 21, the top ofwhich has a piston 22 in a vertical position to take off, position, andprovide pressure to said lid 20 toward the conical ring 19, such that ahermetic seal forms; in the top opening of the hopper 15 rails 24 arewelded and extend diametrically from said hopper's opposite sides in ahorizontal position to allow the handle 21 to slide when the hopper 15is opened or closed; on the opposite end of the hopper there is a secondpiston 23 in a horizontal position to slide the handle 21 over saidrails 24; it is worth mentioning that on lid 20 there is a rectangularplate 17 in a vertical position, having an elliptical boring to preventthe axle of the second piston 23 from bending when the lid is set on thehopper 15. The bottom end of the hopper 15 is connected to the top partof one of the ends of the organic and inorganic waste intake chamber 11by a conventional coupling 25.

The organic and inorganic waste intake chamber 11, which allows theintake of the waste, extracts the air and oxygen that accompanies thewaste, preventing the thermal shock of the waste entering the system, iscomposed of a metallic hollow cylinder 1 in a horizontal position,resistant to a vacuum pressure of −0.56 Kg/cm²; which has in itsinterior a waste mixing assembly 26 in a horizontal position, which iscomposed of a square shaft 8 that has perpendicular rectangularprojections 9 diagonally throughout the length of its four sides (as isclearly shown in FIG. 2). The mixer assembly 26 is fixed to cylinder 1through the end sides of the square shaft 8. For this purpose, both endsof the square shaft 8 join the discs 36 in a vertical position, whichhave a square connector 58 in their centers, having a square cavity 58on their center with dimensions sufficiently large to allow an end ofthe square shaft 8 to be introduced tightly. One of the connector discs36 joins, on the opposite side where the square cavity 58 is, a seconddisc 49 with the same dimensions as the first disc 36; wherein thesecond circular piece 49 has on the face opposite to the face thatconnects the first disc 36, a central round shaft 32, in a horizontalposition to enter into a conical axle box 28, wherein said axle boxattaches to the hatch 27 of the waste intake chamber 11. The centralround shaft 32 has an internal duct 40 in a “U” shape, horizontallyplaced, so that refrigeration liquid can flow and said shaft will notdilate by increase temperature. Said central round shaft is embraced bya cooling device 29; followed by a bearing 30 to fix the round shaft 32;and a notched wheel 31 to allow said square shaft 8 to rotate through achain 33 coupled to a motor 35 (See FIG. 3). The connecting disc 36 onthe other end of the square shaft 8 connects a circular piece 50 on itsface opposite to its square cavity 58; wherein said circular piece 50has on its center a horizontal round shaft 51 that enters an axle box 52to allow rotation and support the central round shaft 51, as this shaftis suspended and fixed because of braces 64, which are metallicprojections extending from the internal wall of cylinder 1 toward theaxle box 52, on opposite end of said axle box there is an axial block 43which works as a lid preventing dust and residue from entering the axlebox and fixes the central round shaft 51. The open ends of cylinder 1are sealed by hatch 27 and 44 (see FIG. 3), wherein the left hatch 27 isfixed to the chamber by a conventional coupling 26 a in front of thecooling device 29. On the end where the right hatch 44 is placed, a ring41 is welded on the edge of cylinder 1 beforehand, which, on itsinternal edge a 10 perimetral cut-in 42 resembling a conical ring, onwhich is fixed, on the top edge of said cut-in 42, a calibrated cylinder53 in the interior of which a solid cylindrical interconnection valve 10slides, which valve has at the same time a 10 cut-in on its left side sothat when it couples with the ring's 41 cut-in 42 there is a hermeticseal (see FIG. 3), in the middle of valve 10 perimetral circular canalthat houses a teflon ring 54 to increase tightness of the hermetic sealon the calibrated cylinder 53; right hatch 44 is fixed to the right endof the calibrated cylinder, whose outer diameter is greater than thecylindrical body 1, matching that of the ring 41, to achieve a fittingbetween both pieces; a ring-shaped piece 45 is added to the center ofthe right hatch 44 with an internal mechanism that prevents air fromcoming inside the cylindrical body 1; finally, the axle of an actuatorpiston 46 is introduced in the center of the ring-shaped piece 45 tothrust the interconnection valve 10 inside of the calibrated cylinder.The cylindrical body 1 has on its top (see FIG. 4) an extraction tower37 of air and volatile particles, which are conducted through a pipe 38that conveys them toward a multiple valve 55. Finally, calibratedcylinder 53 has an inferior perforation 48 in order to couple a verticalpipe 47 to connect the intake chamber 11 to the dehydration reactor 2.

The dehydration reactor 2 that eliminates any trace of moisture that theorganic or inorganic waste includes at the moment of entering thesystem, is built similarly to the intake chamber 11, but differs in thatthe dehydration reactor 2 contains an upper rectangular aperture of onethird the diameter of its cylinder, that traverses its own longitude, toobtain a connection with an expansion chamber 12, consisting of a pairof longitudinal metallic 13 rectangular walls, that are verticallywelded, but with an inclination of 15 in the outward directioncommencing at the edge of the longitudinal aperture, with a conicalappearance; of a pair of truncated semi conical transversal metallicwalls 14, arranged in a 90 vertical position with respect the tocylinder, and it is used to cover the apertures at the ends of thementioned chamber; and a half-pipe shaped piece 34 serves as a upper lidto the expansion chamber 12, this expansion chamber 12 allows elevationof water vapors generated by the organic and inorganic solid waste; thusin this case the extraction tower 56 is above the expansion chamber 12.Another variant of this dehydration reactor is that it is placed insidea heat “casing” 59, but not entirely, to provide a temperature of 180inside the dehydration chamber 2, by means of heat generated by a firstgas burner, and gases obtained are expelled to the environment by meansof an escape duct 57 vertically positioned on the upper right end of theheat “casing” 59, it is worth mentioning that it has an externalinsulator layer 61 that precludes heat diffusion and concentrates itinside said casing. In the same way as the intake chamber 11, thedehydration reactor 2 has an interconnection pipe to connect it to thefirst thermal dissociation reactor 3.

Thermal dissociation is initiated on the first dissociation reactor 3,forming a “crude”vapor (consisting of a vapor that has not yet reachedideal temperature of 420 therefore if this vapor would be extracted andcondensed it would form a low calorific power hydrocarbon). This firstreactor whose configuration is the same as that of the dehydratorreactor 2, differs only in that the expansion chamber 60 is on a smallerscale, given that the “crude” vapors that are going to be obtainedrequire less space since they are not that expansive. Another detailabout this first reactor 3 is that the heat “casing” 59 a has aperforation 71 in the right bottom side to connect a gas burner 70 so itprovides a temperature of 280 to the interior of the first reactor 3.Besides heat being conducted toward dehydration chamber 2, this firstreactor is connected to the second thermal disassociation reactor bymeans of an interconnection pipe.

Regarding the second thermal disassociation reactor 4 where the finalthermal disassociation of the organic and inorganic solid waste takesplace. Such second reactor 4 has the same structure as that of the firstreactor 3, but with the exception that in this case, the cylindricalbody has a bigger longitude at its left end (see FIG. 7), longitude ofexpansion chamber 18 does not vary, with the intention of leaving aspace where a cylindrical expansion tower 5 is placed vertically, whichcomprises of a cylindrical body 68 opened on its lower end to obtain aconnection to the cylindrical body of the second thermal disassociationreactor 4, while its upper end is closed; inside cylinder 68 aresituated from bottom to top: a pipe 79, wherein the “crude” vapors areconducted, a filter constituted of a mesh 94 that covers the perforationon cylinder 68, and some metallic rings 93 distributed over the mesh 94,in such a way that they filter thermolytic vapors passing to thecylinder 68, thus preventing the incursion of carbonic particlesoriginated by the disassociation of solid waste; a pipe 81 where thethermolytic vapors enter, a thin plate 92 with a truncated conicalshape, placed in an inverted way, that is to say that, the smallperforation is facing up and the big perforation is facing down, to slowdown the thermolytic vapor ascend, with the help of a cone 91, suspendedby braces 67; suspended on the top part of expansion tower 5 lays asealed reservoir 89, wherein a pipe 83 is coupled to the reservoir'sinferior end, where the water vapor and volatile particles areconducted, is worth mentioning that inside of the sealed reservoir 89,there lays a thin plate 90 with a truncated conical shape inverselyoriented to slow down the ascend of vapors inside the sealed reservoir89, wherein a pipe 87 is placed in the upper end, for the extraction ofwater vapor, thermolytic vapor and air, to be cooled in the heatexchanger 160; (see FIG. 15). Above cylinder 89, there lays athermolytic vapor extraction pipe 85, that conducts the vapor to theheavy hydrocarbons separator 110, (see FIG. 10), is worth noting thatthe expansion tower 5, as well as the cylinder and expansion chamber 18are placed inside a heat “casing” 98, another aspect about this secondreactor 4, is that such heat “casing” 98 has a perforation 101 on itsleft bottom side that connects to a second gas burner 100, providing atemperature of 420 to the interior of the second reactor 4, and insidethe expansion chamber 5, and in the top part there lays an escape duct84 that allows flow of the combustion gases of the burner 100 into theatmosphere, there is an insulator layer 97 on the exterior of “casing”98 that permits the concentration of heat and avoids its loss. Insidesecond reactor 4 there is a mixing assembly, that in contrast with firstreactor 3 this one only rotates in one way transporting material towardthe left end of second reactor 4, and in its right end it couples withthe mixing assembly of the extraction chamber 6 of the solid fraction ofthe thermal dissociation, that also couples with the cylinder of thesecond reactor 4; it connects to the extraction chamber 6 by means of aconventional couple 66. The extraction chamber of the solid fraction ofthe thermal dissociation 6, removes these particles from the heatgenerated inside the second thermal dissociation reactor 4; the solidfraction of the thermal dissociation is composed of carbon, ashes,metallic bits, sands, glass bits, among others, that is to say, allwaste that was not susceptible to the thermal dissociation; this chamberis similar in manufacture to the intake chamber 11, and also is heatfree, in the same manner it is provided with an interconnection pipethat connects it to the cooling and extraction chamber 7.

Cooling and extraction chamber 7, is where the solid fraction of thethermal dissociation is cooled in order to be extracted and manipulated,it resembles intake chamber 11, but it houses on its exterior a coolingdevice 113, that cools down the chamber's interior to a temperature ofless than 90 C., its cylinder (see FIG. 9) is provided in its left endwith a sealing system 74 equal to that of hopper 15, with the onlydifference that it is vertically oriented to allow a hermetic sealing,and the extraction of the solid fraction once it cools down, on top ofthe cylinder there is an extraction tower 122 in which the air enteringchamber 7 is extracted, as a result of its aperture.

A heavy hydrocarbons separator 110 (see FIG. 10) and two heatexchangers, where 95 is the primary and 96 secondary; this heavyhydrocarbons separator 110 has a cylindrical shape. Here enter thethermolytic vapors that come from expansion tower 5 coupled to it bymeans of couple 86 and conducted to its interior by pipe 85; inside thisheavy hydrocarbons separator 110 lays a pipe with lateral perforations111 placed in the interior in a vertical way to allow the flow ofthermolytic vapors so they condensate inside of it, from the condensedvapor heavy hydrocarbons are formed (paraffin wax) that solidify at atemperature of 60° C., this separator is not provided with a coolingsystem, due to the fact that only the increment of volume inside thereservoir causes the condensation of thermolytic vapors that give originto the heavy hydrocarbons, these hydrocarbons are extracted later on bythe service lid 112, that is located in the bottom part of separator110, inside there is a conic trap 115 that is a thin plate welded topipe 111 to prevent its elevation, so they can be dragged by theextraction pipes 113 and 114, given that these perforated pipes 113 and114 extract lighten thermolytic vapor to be cooled by means of a heatexchanger 96 secondary or 95 primary, they decrease the thermolyticvapor temperature to 68° C. and conduct it toward light hydrocarbonsseparators 116 or 117, (see FIG. 11), these heat exchangers 95 primaryand 96 secondary are cylindrical shaped reservoir and in its interiorare found serpentine shaped pipes, thermolytic vapor circulates insidethem, inside the reservoirs circulates liquid refrigerant to dissipateheat from the serpentine, these heat exchangers come in pairs and havethe same function and are coupled to the same heavy hydrocarbonsseparator 110 with the intention that in a given state of the reaction,the production of thermolytic vapor is twice the volume than that of themajority of the thermal dissociation process and this accomplishes anoptimal thermolytic vapor extraction, thus an over pressure insideexpansion chamber 5 is avoided, on the other hand this exchangersarrangement serves as a method to provide maintenance when required byone of them, in such a way that the thermal dissociation process in notinterrupted, the thermolytic vapor cooled by heat exchangers, 95 primaryand 96 secondary, is conveyed to the light hydrocarbons separators 116primary and 117 secondary.

Two light hydrocarbon separators 116 primary and 117 secondary that havea cylindrical shape, vertically oriented, sealed on their ends andconstituted of the same components and having in its interior aperforated pipe 118, where the thermolytic vapor cooled down to 68° C.enters, here it is condensed because it its cold and once the volume isincreased inside de reservoir that contains them, that is separator 116primary and 117 secondary, it condenses and forms light hydrocarbons,these separators come in pairs to facilitate the extraction ofthermolytic vapor coming from expansion tower 5 as explained earlier,besides giving the opportunity to provide maintenance to one of themwithout stopping the thermal dissociation system. A trap placed insideseparators 116 primary and 117 secondary prevents condensable vapors tobe extracted, the most volatile vapor is extracted by a perforated pipe120 that transports the most volatile vapor to the vacuum pumps 127primary and 128 secondary that will be explained later, there is ahatchway on the bottom of the cylinder to extract the lighthydrocarbons.

A multiple valve 55 that has a cylindrical shape, it is comprised of asolid cylindrical body, that houses in its interior a network of ducts,so that the connection accessories, temperature readers and actuatorscan be distributed; has couples on one of its ends that couple to theextraction tower 37 of the organic and inorganic solid waste intakechamber 1, by means of couple 39, it also connects extraction tower 63of the third reactor 3 by a couple 65, also it connects on this end tothe extraction tower 122 of the cooling chamber 7, by means of a couple123 on the other end are placed the connections to expansion tower 5that couples to it by means of couple 78 that is placed on the bottompart of expansion tower 5, also there is a couple 80 placed on themiddle part of the expansion tower 5, and one more connects at this endto the water vapor and volatile particles heating cylinder 89. On to topof the multiple valve 55 we can find three oxygen sensors 124 thatdetermine the amount of “free” oxygen (oxygen that is not part of amolecular chain) of the vapor that arrives to this multiple valve 55 andin this way it determines if this vapor is sent, with the help of valves125, to the water vapor and volatile particles heating cylinder 89, andthus avoiding thermolytic heat oxidation within the expansion tower, themultiple valve is also provided of temperature readers 126 that helpmeasuring vapor temperature and thus determining if they are “crude”vapors or thermolytic vapor, in case of it being “crude” vapor, with thehelp of the actuators valves 125, it will redirect them to the lowerpart 78 of expansion tower 5, in case that the vapors have a temperatureof 420° C. it will be considered a thermolytic vapor and will onlyrequire a slight residency inside the expansion tower 5 and thus withthe help of actuator valves 125 will be directed toward the middle partby means of couple 80, to the expansion tower 5.

Two vacuums pumps 127 primary and 128 secondary; will provide the vacuumpressure of −0.56 Kg/cm² required in the interior of the system andbesides that they also suction vapors from the inside of the extractiontowers and expansion tower 5 with the help of the multiple valve 55completing primary and secondary extraction systems respectively. Acapturing reservoir of chlorine gas particles that has a cylindricalshape that contains a saline solution 130 H₂O+(NaCl) to capture chlorineparticles that can be dragged by volatile vapor formed by a mixture ofcombustible gases, we call this mixture “synthetic” gas. On the bottompart of the reservoir 129 is where the synthetic gas enters to be mixedmomentarily with the solution 130, in this way trapping the chlorineparticles in the solution, the “synthetic” gas is extracted fromreservoir 129 by means of a pipe 131, that conveys it to anotherreservoir 141 that connects to it by means of couple 132, and it isplaced on top if this reservoir.

There is a third heat exchanger 138, a liquids separator 139, with acylindrical shape and comprised of the same components as the lighthydrocarbon separators 116 and 117, and a vacuum pump 140, this heatexchanger 138 is coupled to the air and volatile particles heatercylinder 89 that is placed inside expansion tower 5, connects to it bymeans of couple 88 to extract hot vapors coming from the air andvolatile particles heater cylinder 89, to be cooled down by heatexchanger 138 to a temperature of 68° C. and once they cool down theycondensate to form a mixture of water with light hydrocarbons that lateron is treated to separate light hydrocarbons from water and added to thelight oil recovered by separators 116 primary and 117 secondary.

A confiner reservoir of sulfur particles 141, that has a cylindricalshape and contains a solution 142 composed of calcium hydroxide Ca(HO)₂and water, to trap any trace1 of sulfur molecules, the “synthetic” gasenters the cylinder on its bottom side, where the solution is restingand as the gas passes through the solution they mix momentarily trappingthe sulfur particles that the “synthetic” gas contains, the clean gas isextracted later on from this reservoir by means of a pipe 143 that iscoupled to a drying filter 145 that traps in any humidity that the“synthetic” gas might have, next it is stored in collector tank 146 andthus this “synthetic” gas can be used as fuel for heaters 100 and 70 ofthe forth 4 and third 3 reactors respectively.

Method to Obtain Hydrocarbons from Organic and Inorganic Solid Waste,Introduced in the Thermal Dissociation System, Consisting of:

Preparation of raw material, given the diversity of the waste, it isrecommended a pre-selection, given that ferrous, glass and sand wasteare not susceptible to thermal dissociation, and in case they access thesystem they would occupy a valuable space, but they do not affect thefunctionality, and given that there is waste with ferrous and glassmixtures, they will not be excluded because they can be processed toobtain a hydrocarbon from the fraction that is susceptible to thethermal dissociation, remaining, without any alteration the materialthat are not susceptible to the thermal dissociation, not being theselection indispensable, to obtain hydrocarbons from organic andinorganic solid waste, once the waste bits have been selected, thosebeing of a bigger size than that of the superior aperture 16 of hopper15 must be crushed by means of a conventional crusher, to allow itsaccess, besides all waste that can be reduced in volume, this with theintention of increasing the system's capacity, it is worth mentioningthat crushing is not indispensable for the system; waste is transportedto the intake hopper 15 by means of a conventional dispenser, organicand inorganic solid waste enters through the hopper's 15 superioraperture 16, this is accomplished by means of the extraction mechanism76, that retracts lid 20 where the actuator piston 22 retracts thering's 19 lid 20 and by means of a second piston 23, slides the lidleaving the hopper's apertures free, waste gets inside intake chamber 11which is at ambient temperature with the intention of impeding a thermalshock that could form toxic compounds like dioxins, that is coupled onthe top to hopper 15, that was previously sealed on its opposite side byinterconnection valve 10, at the same moment as the waste enters, themotor 35 starts working to rotate the mixing assembly, with theintention of transporting and accommodating the waste inside the intakechamber 11, once they fill all the space inside such chamber, proceedsthe sealing of the hopper 15 with the retraction mechanism 76 that isactivated inversely, the piston 23 pushes the lid 20 over the ring 19and the piston 22 pushes toward the ring 19 allowing a hermetic seal ofthe system, avoiding any intrusion of air inside the intake chamber 11,once the chamber is sealed the mixing assembly continues to rotatealternating its direction every 60 revolutions, meanwhile by means ofthe extraction tower 37, air and volatile particles that accompany thewaste, they are suctioned by the action of the vacuum pump 140 thatgenerates a vacuum inside the intake chamber of −0.56 Kg/cm², thissuction is carried out from the multiple valve 55, that later on arepassed to the heating cylinder 89 that is located inside the expansiontower 5, that has a temperature of 420, given that heating the air andvolatile particles in a sudden manner dissociates the molecular bonds toform a thermolytic vapor, that also may contain pathogen agents likeviruses and so forth, that would be killed when exposed to thistemperature and would also form a thermolytic vapor, from here they aredirected toward the heat exchanger 138 that cools down the air andthermolytic vapor to a temperature of 68 C., later on it is directed toa liquids separator 139 where once it cools down condensates leaving aliquid hydrocarbon sediment mixed with small water particles, the mostvolatile fraction is suctioned from the separator by means of a vacuumpump 140, that directs it to a gas purifier 129, here it mixes with thesolution 130 that captures any trace of chlorine particles and later onit is directed to a gas purifying reservoir 141 where the gas mixes withthe solution 142 to capture any trace of sulfur, then it is directed tothe moisture filter 145, leaving a clean gas that can be stored in anaccumulation reservoir 146 to be used later on as combustible forburners 70 and 100. Besides, the mixing assembly helps to get rid of airand volatile particles from the waste that is going to be processedgiven that it is in constant movement, the mixing assembly plates 9break any air bubbles encapsulated inside the organic and inorganicwaste, thus avoiding oxidation of the waste inside the system. Theresidency time of the organic and inorganic solid waste inside thechamber 11 to get rid of any trace of air and volatile particles isdetermined by the time it takes to reach −0.56 Kg/cm² inside the chamberand an additional 50% of residency time is added, for example if it took10 minutes then 5 minutes are added, during all this time the vacuumpump 140 is suctioning and the mixing assembly alternating rotation.Finishing the residency time, suctioning is stopped inside the intakechamber 11 and the mixing assembly rotates on a displacement way toconvey the waste to the interconnection valve 10, that is coupled to thering 41, and by means of actuator piston 46 retracts the valve allowingit to be slide through the calibrated cylinder 53, in this way the wasteleaves the intake chamber 11, thanks to the bottom perforation 48 of thecalibrated cylinder 53 in which an interconnection vertical pipe 47 iscoupled, and in its opposite side directs the waste to the dehydrationchamber 2, once chamber 11 is discharged the interconnection valve 10 isreturned to its hermetic sealed position, and once again filling of theintake waste chamber 11 takes place, this is a semi-continuous process.

Dehydration of organic and inorganic solid waste takes place by means ofa waste dehydration chamber 2, waste directed from the intake chamber 11propelled by the mixing assembly fall out inside the dehydration chamber2, the chamber has been preheated to 180 C. at the moment that the solidwaste enters, it is worth mentioning that this temperature is reacheddue to a gas burner that heats the exterior of the cylinder and in thisway it protects the waste from the direct flame avoiding its combustion,heat is conducted by a heat “casing” 59, besides this chamber is under avacuum of −0.56 Kg/cm², with the intention of getting rid of anymoisture trace that may accompany the waste, in the interior we find themixing assembly alternating rotation, in the same way as the intakechamber 11, with the only difference that this assembly helps to diffuseheat among all waste, thus reducing residency time inside this chamber,also the water vapor generated elevates from the cylinder to theexpansion chamber 12, allowing an easier separation and a quickliberation of moisture that they may carry. In this way waste enteringthis chamber 2 absorbs heat contained within, lowering the internaltemperature and preventing a thermal shock, it also allows a gradualtemperature increment preventing an over production of water vapor thatwould cause an unwanted over pressure inside of the thermaldissociation, during all this time vapors are being suctioned with thehelp of the vacuum pump 140, and by means of extraction tower 56 aredirected to the multiple valve 55, and later on to the cylinder 89 aswell as the air and volatile particles of intake chamber 11, itssubsequent process is the same as the one described before; residingtime inside the dehydration chamber 2 depends on the heat absorptiontime, that is to say that, once the waste enters, the temperature withinthe chamber decreases, then the time it takes to reach a temperature of180 C. once again is measured and then a 50% more is added, for example:if it takes 6 minutes to absorb the heat then 3 more minutes are added,this is the ideal residency time that varies depending on the kind ofwaste being processed, during all this time the mixer assembly keepsalternating rotation, once the residency time ends it is directed to theinterconnection valve 10 of the dehydration chamber 2, it retracts andallows the discharge of the waste to the first thermal dissociationchamber 3, later on once such chamber is discharged, the valve returnsto its sealed position, in such a way that once again the waste comingfrom intake chamber 11 is introduced on its top side so it can bedehydrated.

Thermal dissociation of organic and inorganic solid waste takes placeinside first thermal dissociation chamber 3, wherein formation of avapor takes place from which hydrocarbons are recovered from organic andinorganic solid waste, in a such a way that the waste enters through theinterconnection pipe 47 to the interior of the first thermaldissociation reactor 3, previously pre-heated to a temperature of 280°,in the same way as in the dehydration chamber 2 once the waste enters,the temperature inside drops because it absorb heat, and the residencytime is determined in the same way as in the previous chamber, also themixing assembly keeps alternating its rotating orientation, with thedistinctiveness that in this first reactor 3, heating the waste mixtureoriginates its thermal dissociation, in such a way that a “crude” vaporis formed consisting of molecular chains that once condensed form a lowcalorific power hydrocarbon, this vapor is separated from the wastemixture inside the first reactor 3, ascending inside an equal atmospherein the expansion chamber 60, in order that the dissociation takes placein a faster rate, and with less fuel consumption, this vapor isextracted by the extraction tower 63 and directed to the multiple valve55 where the temperature and “free” oxygen level are measured, “crude”vapor is determined by means of the oxygen sensors 124, and thetemperature by means of thermometers 126, in case that this vaporcarries some trace of “free” oxygen it is directed to the lower part ofthe expansion tower 5 by means of pipe 79, so this “crude” vapor can beheated to create a thermolytic vapor, this vapor carries a temperatureof 420° C. and from it high calorific power hydrocarbons can form, oncethe residency time inside the thermal dissociation reactor 3 is over, a“viscous mass” is formed from the organic and inorganic solid wastesubjected to the thermolytic dissociation, inside the reactor this wastemelts, creating a homogeneous mixture, constituting a “viscous mass”from which not all the hydrocarbons have been extracted yet, this massis directed to the end of first reactor 3 where the interconnectionvalve 10 is located, which in turn retracts allowing the flow toward thesecond thermal dissociation reactor 4, once the first reactor 3 isdischarged an hermetic sealing forms by means of the valve 10, thusallowing the access of waste coming from the dehydration chamber 2 andcontinue with the process.

Thermal dissociation takes place in two reactors, in such a way that inthe first reactor temperature is gradually risen to 280 C., commencingfrom this temperature the majority of the “crude” vapor generation takesplace, consequently the waste is directed to a second thermaldissociation reactor 4, that has been pre-heated to a temperature of 420C. This is the ideal temperature to form high calorific powerhydrocarbons, in this second reactor all the material susceptible to thethermal dissociation is transformed into thermolytic vapor, that ascendsto the expansion chamber 18 with the help of the mixing assembly fromthe second reactor 4, with the distinctiveness that this assemblyrotates only in one direction transporting the processing material tothe end where expansion tower 5 is located, this mixer assembly helps toseparate vapors generated by the thermal disassociation given that theplates blend the mixture in such a way that it helps releasing thethermal vapor from the solid fraction of the thermal dissociation,composed of: carbon, ashes, metallic bits, glass and sand; the vaporgenerated on this second reactor 4 is extracted through the extractiontower 73 and conducted toward the multiple valve 55 that determines thevapor's temperature and directs it toward the expansion tower 5 that iscoupled on the end of the second reactor 4, here the “crude” andthermolytic vapors stay the necessary time to homogenize so an idealthermolytic vapor can be obtained from which high calorific hydrocarbonscan be formed. The thermolytic vapor extracted from the expansion tower5 is directed toward a heavy liquid hydrocarbons separator 110 where theheavy molecular chains are separated from the lighter and volatile onesto form a heavy liquid hydrocarbon (paraffin wax), this takes place dueto the expansion of a vapor on a hermetic container, and the lightervapor is extracted from such separator to be cooled down by the heatexchangers 95 and 96 (from this point on the vapor extraction line ofthe system is provided with twice the devices forming a doubleextraction line composed of heat exchangers, light hydrocarbonsseparators and vacuum pumps, these lines are finished at the gaspurifier 129, this with the intention of coping with any over-productionof thermolytic vapor inside the system, also permitting maintenancewithout bringing the process to a halt), the heat exchangers 95 and 96cool the vapor down to 68 C., this is the temperature where the vaporscondensate and are trapped in the light hydrocarbons separators 116 and117, where the lighter chains are separated from the volatiles ones toform a light liquid hydrocarbon, the more volatile (“synthetic” gas) isextracted from these separators by means of the vacuum pumps 127 and128, they extract the generated vapors and direct them toward apurifying reservoir 129, where they mix with a solution 130 and after amomentary combination, the chlorine particles that might have beencarried by the “synthetic” gas are trapped, then this gas is directed toa purifying reservoir 141 that contains a solution 142 and in the sameway as before the sulfur particles that might have been carried by the“synthetic” gas are trapped, this gas is directed toward a moisturefilter 145 where this gas is dried out so it can be stored on anaccumulation reservoir 146, to be used later on as fuel for the burners100 and 70, achieving a cost-effective system process, besides beingenvironmentally safe, given that the emissions of the combustion of this“synthetic” gas are not harmful to the atmosphere. In this way thesystem operates in a very safe and efficient way, in a closed circuit,preventing the contact of the thermolytic gas with the environment. Theresidency time of the matter inside of the second thermal disassociationreactor 4 is calculated by the time it takes to the processing materialto absorb the heat, given that once the material coming from the firstthermal dissociation reactor 3 enters the second reactor 4 thetemperature drops and it takes some time to reach a temperature of 420C. again, to this time a 75% is added, for example if it takes 10minutes then 7.5 minutes of residency are added.

Residues of the solid fraction of the thermal dissociation composed ofcarbon, ashes, metal bits, glass and sand that were not subjected to thethermal dissociation, are taken away from the heat of the second thermaldissociation reactor 4 with the help of the mixing assembly shared bythe extraction chamber 6 and the second reactor 4, this extractionchamber 6 takes away the solid fraction from the heat of the secondreactor, achieving this with the help of the mixing assembly thatrotates inversely transporting the waste toward the interconnectionvalve of the extraction chamber 6, the valve retracts and allows theflow toward the cooling chamber 7 of the solid fraction of the thermaldissociation, where the fraction cools down to a temperature of 90 C. soit can be handled, with the help of a cooling system 113 that circulatesa liquid refrigerant that dissipates out the heat inside the chamber,that is hermetically sealed on one end by the interconnection valve ofthe extraction chamber 6, and on the opposite end by the sealingmechanism 74. It is worth mentioning that on this end the solid fractionof the waste is extracted to separate the metals, glass bits and sandsand to only leave a mixture of carbon and ashes that is stored on theconventional sacks, to be distributed and traded later on; it is worthmentioning that during the extraction of the solid fraction from thischamber, air enters inside the cooling chamber 7, once it is sealed bythe sealing mechanism 74 air is extracted by means of the extractiontower 122, that directs it toward the multiple valve 55 redirecting themtoward the cylinder 89, that heats this air and once it is extracted itcools down to a temperature of 68 C. on the heat exchanger 138, then itis directed to the separator 139 where any trace of moisture iscondensed and later on the more volatile gas is extracted by means ofvacuum pump 140, then to a drying filter 146, and finally to anaccumulator reservoir 145. This air is mixed with the “synthetic” gasachieving an excellent combustion.

What is claimed is:
 1. A system for obtaining hydrocarbons from organic and inorganic solid waste comprising: a hopper for receiving solid waste disposed on a waste intake chamber; said intake chamber operated at ambient temperature comprising a first mixer assembly for mixing and conveying the solid waste through said intake chamber and an extraction tower for air and volatile particles; a dehydration reactor preheated to a temperature of 180° C. for receiving the solid waste from said waste intake chamber; said dehydration reactor comprising a second mixer assembly and an expansion chamber and extraction tower for water vapor; a first thermal disassociation reactor connected to said dehydration reactor; said first thermal disassociation reactor preheated to a temperature of 280° C., and maintaining a vacuum pressure of −0.56 Kg/cm² to form crude vapors and comprising an expansion chamber and extracting tower; a second thermal disassociation reactor in series with said first thermal disassociation reactor to form thermolytic vapors, and comprising an expansion chamber and extracting tower; an extraction chamber for a solid fraction of a solid waste received from said second thermal disassociation reactor; a cooling chamber for cooling said solid fraction of the solid waste received from said second thermal disassociation reactors; an expansion tower to form an ideal thermolytic vapor comprising a vapor and volatile particles heating cylinder; a first cylinder for separating heavy hydrocarbons received from said first and second thermal disassociation reactors; said first cylinder disposed between a first and a second thermolytic vapor heat exchangers; a second and a third cylinder for separating light hydrocarbons; said second cylinder connected to said first thermolytic vapor heat exchanger and said third cylinder connected to said second thermolytic vapor heat exchanger; a fourth cylinder for separating liquids; a third heat exchanger attached to said fourth cylinder; a first and a second synthetic gas purifying reservoirs for purifying gas; three vacuum pumps connected to said first synthetic gas purifying reservoir; a first of said three vacuum pumps connected to said second cylinder; a second of said three vacuum pumps connected to said third cylinder; a third of said three vacuum pumps connected to said fourth cylinder; a synthetic gas accumulating reservoir attached to said second synthetic gas purifying reservoir; and a multiple valve comprising one or more temperature readers and one or more oxygen sensors that determine the temperature and oxygen content of crude and thermolytic vapors coming from one or more extraction towers and one or more expansion towers through a network of ducts, said multiple valve distributing the crude and thermolytic vapors with one or more actuator valves to either said vapor and volatile particles heating cylinder or a lower part of said expansion tower or a middle part of said expansion tower to form an ideal thermolytic vapor depending on their oxygen content and temperature in order to optimize the production of hydrocarbons.
 2. A semi continuous method to obtain hydrocarbons from organic and inorganic solid waste comprising: preparing raw material; selecting waste that is susceptible to thermal dissociation; filling an intake chamber, which is at ambient temperature, via a dispenser through a superior aperture of a hopper via an extraction mechanism on a hopper lid; leaving the aperture of the hopper free of any waste; sealing the intake chamber hermetically via the hopper lid; distributing the waste inside the intake chamber by means of a mixing assembly; creating a negative vacuum pressure in the intake chamber by extracting air and volatile particles via a vacuum pump; removing and breaking down air bubbles via the mixing assembly and achieving a vacuum pressure of −0.56 Kg/cm²; directing the solid waste to a dehydration chamber via the mixing assembly that propels it to the end of the intake chamber, where an interconnection valve is located that allows the flow of the waste and from the intake chamber to the dehydration chamber, via a vertical interconnection pipe; dehydrating the waste inside the dehydration chamber; preheating the dehydration chamber to a temperature of 180° C.; creating a constant vacuum pressure of −0.56 Kg/cm² in the dehydration chamber; removing and releasing moisture out of the solid waste as water vapor through an extraction tower and allowing the separation of the moisture from the dehydrated solid waste, such waste remaining on the bottom of the dehydration chamber; transporting the dehydrated waste to a first thermal dissociation reactor, thermally dissociating the organic and inorganic solid waste via the first thermal dissociation reactor pre-heated to a temperature of 280° C., and maintaining a vacuum pressure of −0.56 Kg/cm², which forms a “crude” vapor; extracting the “crude” vapor via a vacuum pump; directing the crude vapor extracted from the first thermal dissociation reactor to a multiple valve that confirms the presence of crude vapor and then directs the crude vapor to an expansion tower that heats the crude vapor to form an ideal thermolytic vapor; transporting the remaining solid waste from the first thermal dissociation reactor to a second thermal dissociation reactor via a mixing assembly of the first reactor that propels the waste toward a second interconnection valve that allows the flow of the waste between the first thermal dissociation reactor and the second thermal dissociation reactor and also provides hermetic sealing between the reactors; pre-heating the second thermal dissociation reactor to a temperature of 420° C. and maintaining a vacuum pressure of −0.56 Kg/cm²; separating a thermolytic vapor from the thermal dissociation of the solid fraction, leaving this fraction deposited inside the second thermal dissociation reactor; extracting the thermolytic vapor from the second thermal dissociation reactor by means of a vacuum pump; directing the thermolytic vapor to the multiple valve that determines and directs the vapor toward an expansion tower where the thermolytic vapor stays to form more ideal thermolytic vapor; heating the thermolytic vapor by means of the expansion tower coupled to the second reactor, such tower is heated to a constant temperature of 420° C. and maintaining a vacuum pressure of −0.56 Kg/cm²; extracting the ideal thermolytic vapor from the expansion tower by means of a pipe located on top of the expansion tower; separating heavy liquid hydrocarbons from lighter hydrocarbons present in the ideal thermolytic vapor, by means of a separator that separates the ideal thermolytic vapor in a heavy liquid hydrocarbons separation reservoir, where the vapor enters and condensates due to the expansion inside this reservoir; cooling the lighter hydrocarbons left in the ideal thermolytic vapor; dividing light hydrocarbons from volatile hydrocarbons by condensing the light hydrocarbons to form a light hydrocarbons liquid; suctioning the volatile hydrocarbons, by means of one or more vacuum pumps that suction the volatile hydrocarbons; directing the volatile hydrocarbons to a separator and a heat exchanger, and a purifying reservoir; capturing the chlorine of a “synthetic” gas inside of a purifying “synthetic” gas reservoir wherein a solution of H2O+(NaCl) is found, that liberates the “synthetic” gas from any trace of chlorine particles; capturing the sulfur from the “synthetic” gas, inside the purifying “synthetic” gas reservoir wherein a solution of Ca(HO)2+H2O is found, that at the moment of mixing momentarily with the “synthetic” gas liberates the “synthetic” gas from any trace of sulfur particles; eliminating the moisture from the “synthetic” gas by means of a filter that captures any moisture carried by the gas; storing the “synthetic” gas inside an “synthetic” gas accumulation reservoir where it is stored momentarily to be used later on as a combustible for burners of the system; transporting the solid fraction of the thermal dissociation composed of carbon, ashes, ferrous bits, glass, and sands, that are extracted from the second reactor toward an extraction chamber, via the mixing assembly; coupling the extraction chamber to one end of the second reactor to release the solid fraction from the heat that is propelled toward the interconnection valve which allows the flow of the waste between the second thermal dissociation reactor and the extraction chamber; transporting the solid fraction of the thermal dissociation from the extraction chamber toward a cooling chamber via the mixing assembly of the extraction chamber that propels the solid fraction toward the interconnection valve that allows the flow of such fraction between the extraction chamber and the cooling chamber; providing an hermetic seal between the extraction chamber and the cooling chamber; cooling the solid fraction of the thermal dissociation by means of the cooling chamber with a cooling system that dissipates the heat from inside; extracting the solid fraction of the thermal dissociation by means of the cooling chamber provided in its interior with a mixing assembly, that propels such fraction toward the end where a sealing mechanism is located, in a retracted state, and thus propelling such fraction to the exterior of the cooling chamber; and separating the solid fraction of the thermal dissociation comprising a mixture of carbon, ashes, ferrous bits, glass via a sieve it separates non-ferrous bits and with an electromagnet ferrous bits.
 3. The semi continuous method of claim 2, wherein bigger sized chunks of solid waste used for filling in the intake chamber are triturated at the top part of the aperture of the hopper before being placed inside the intake chamber, thereby reducing the volume of the waste. 